Selective methylation of phenols

ABSTRACT

Vapor phase methylation of phenols with methanol in contact with a vanadium oxide catalyst which may additionally contain iron oxide and at least one other oxide of magnesium, titanium, manganese, beryllium or boron.

United States Patent [1 1 Nakajima et al.

[4 1 Dec. 17, 1974 SELECTIVE METHYLATION OF PHENOLS [73] Assignee: Asahi Kasei Kogyo Kabushiki Kaisha, Osaka, Japan [22] Filed: Dec. 13, 1971 [21] Appl. No.: 207,546

[30] Foreign Application Priority Data Dec. 11, 1970 Japan 45-109385 Dec. 17, 1970 Japan 45-112490 Dec. 17, 1970 Japan r. 45-112491 [52] U.S. Cl 260/621 R, 252/432, 252/461, 252/471, 252/475, 260/620 [51] Int. Cl. C07C 37/16 [58] Field 01 Search 260/62] R, 624 C, 620; 252/432, 461, 471, 475

[56] References Cited UNITED STATES PATENTS 2.091.483 8/1937 Olin 260/624 C X 2,435,087 1/1948 Luten et a1 260/621 R X 2,910,515 10/1959 Luvisi et a1. 260/624 C X 3,479,410 11/1969 Hamilton 260/621 R 3,642,912 2/1972 Sharp 81 a1 260/621 R FOREIGN PATENTS OR APPLICATIONS 603,254 5/1961 Belgium 260/624 C Primary Examiner-Leon Zitver Assistant Examiner-Norman P. Morgenstern Attorney, Agent, or Firm-Cooper, Dunham, Clark, Griffin & Moran [57] ABSTRACT Vapor phase methylation of phenols with methanol in contact with a vanadium oxide catalyst which may additionally contain iron oxide and at least one other oxide of magnesium, titanium, manganese, beryllium 0r boron.

18 Claims, N0 Drawings SELECTIVE METHYLATION OF PHENOLS BACKGROUND OF INVENTION This invention relates to a catalytic process for the methylation of the ortho position of phenols having at least one ortho hydrogen and to certain novel catalysts useful in the process.

Compounds such as those represented by the general formula:

are of known utility. They are especially useful in the preparation of polymers such as polyphenylene oxide. 1n the formula each R is a monovalent substituent selected from the group consisting of hydrogen, methyl, phenyl, and methyl substituted phenyl.

Methods are already available for the alkylation of phenols in the ortho position. They are described, for example, in British Pat. Nos. 717,588 and 1,112,914; U.S. Pat. No. 3,446,856; Japanese Pat. Publication Nos. 27367/1964 and 29293/1970; and in the report by Enomoto et al. in the Catalyst Research Conference of 1968.

British Pat. No. 717,588 relates to an alkylation process in which a metal oxide having dehydrating action such as the oxides of aluminum, thorium, zirconium, zinc, iron, manganese, magnesium or calcium are employed as catalysts. The process is not completely satisfactory, however, because it is not sufficiently selective. For example, the methyla-of phenol leads not only to the desired ortho-substituted products but also to undesirably large amounts of the meta and para isomers. The separation of the undesired byproducts is complicated and expensive, but they must be separated especially if the desired product, 2,6-xyleno1 is to be used for the production of polyphenylene oxide.

U.S. Pat. No. 3,446,856 describes the alkylation reaction using magnesia as a catalyst. This is a somewhat improved procedure, but the elevated temperature, e.g., 475C. at which it is carried out leads to excessive decomposition of starting materials such as phenol and methanol.

British Pat. No. 1,112,914, Enomotos method, and

the above identified japanese Patent Publications all relate to improved processes in which the magnesia is enriched with a second or third element. With relatively inexpensive additives there is still appreciable decomposition of the starting materials which is often accompanied by a marked decrease in the activity of the catalyst. The addition of rare earth metals or of uranium or palladium is helpful, but it is also expensive.

Despite extensive research no completely satisfactory method has yet been found for the orthomethylation of phenols.

THE INVENTION It has now been discovered in accordance with this invention that phenols can be methylated in the ortho position with methanol using a vanadium oxide catalyst in a vapor phase reaction at elevated temperature. The use of vanadium oxide results in methylation almost exclusively at the ortho position. Moreover, there is reduced decomposition of methanol and increased catalyst life. The use of iron oxide in association with the vanadium oxide leads to improved results. The addition of an oxide of magnesium, titanium, manganese, beryllium, boron, or mixtures of these oxides to produce a polymetallic catalyst results in even greater improvements. These polymetallic catalysts are novel and are specifically included within the scope of this invention.

A further feature of the invention is the discovery that the addition of water vapor to the reaction system in the amount of from about 2 to 12 mols per mol of the phenol utilized helps to prevent the catalysts from breaking down into finer particles or powders which clog the reactor. Thus the life of the catalyst is extended, and the periods between shut downs of the operation to clean the reactor are prolonged.

The term oxide as used in association with various metals in describing and claiming this invention refers to all of the several oxides of the metal known to exist such as V 0 V 0 V 0 VO, Fe O FY2 0 FeO, MgO, TiO MnO MnO, Mn O and to mixtures of these various oxides.

1n the bimetallic vanadium-iron catalysts used in this invention the atomic ratio of iron to vanadium is normally from about 9 to l /9. The preferred range for optimum results is from 4 to H4. When at least one compound selected from the group consisting of oxides of manganese, magnesium, titanium, beryllium and boron is added, the atomic ratio of vanadium to iron to other metal or mixture of metals is from about 1/9 9 1 z 1 0.01. The preferred range in polymetallic catalysts is l/44:1:l-O.l.

Vanadium and any of the other metals used in the present invention may be obtained from any of their usual compounds such as nitrates, hydroxides, carbonates, oxalates, halides, and the like. They may be converted to the desired oxides by immersing, mixing, coprecipitation or other conventional methods. The methods for preparing the catalysts are illustrated in the examples. In actual use they may be supported on suitable carrers such as alumina, silica, silica-alumina, and the like.

In accordance with the process of the invention a mixture of methanol and the selected phenol is contacted with the catalyst in the vapor phase at an elevated temperature to methylate the phenol at one or both of the ortho positions. A mixture of methanol and phenol, for example, can be converted predominantly to ortho cresol or to 2,6-xylenol, or to a mixture of these compounds.

Phenols which may be methylated by the process of this invention include, for example, phenol itself, 0- cresol, m-cresol, p-cresol, 2,3-xylenol, 2,4-xylenol, 2,5- xylenol, 3,5-xylenol, 2,3,4-trimethylphenol, 2,3,5- trimethylphenol, 3,4,5-trimethylphenol, 2,3,4,5- tetramethylphenol, O-phenylphenol, p-phenylphenol, 2-tolylphenol, 2,4-diphenylphenol, 2,3- diphenylphenol, 2-xylylphenol, 2-mesitylphenol, 2- durylphenol, 2-phenyl-4-methylphenol, 2-tolyl-4- phenylphenol, 2-phenyl-4-tolylphenol or S-methyl- Sphenylphenol. All of these phenols may be represented by the formula wherein each R is a nonvalent substituent selected from the group consisting of hydrogen, methyl, phenyl, and methyl substituted phenyl.

Any one or a mixture of the above phenols is vaporized together with methanol and passed through a reactor containing the selected catalyst. The reactor may take any of the usual forms such as stationary bed, moving bed, fluidized bed, and the like. The reaction temperature is typically in the range of from about 250C. to 450C., with the preferred range being from 300C. to 400C. At temperatures appreciably lower than 250C. there is a noticeable decrease in yield, and as the temperature increases much above 500C. there is an appreciable increase in the amount of byproducts produced, especially byproducts which are methylated in positions other than the ortho position. There is also a noticeably increase in decomposition of methanol.

A particular advantage of the process of this invention is that it can be carried out at a relatively low temperature compared to known methods so that the cost of operation is decreased. Additionally there is less decomposition of starting materials or products, and the catalyst life is markedly increased.

While some methylation is effected even with small amounts of methanol, it is preferred that there be at least one molar equilvalent of methanol for each unsubstituted ortho position in the phenol to be methylated. Normally the molar ratio of methanol to phenol type reactant is from about 1:1 to :1. There is little advantage to increasing the molar ratio appreciably above 10:1 since the change in yield does not compensate for the additional cost.

The presence of a reaction inert gas such as nitrogen, hydrogen, carbon monoxide, carbon dioxide or methane is often helpful. As mentioned above the use of water vapor helps to extend the life of the catalyst even longer than usual. When used, it may be employed in a water vapor-phenol reactant mole ratio of from about 2:1 to 12:1. When the amount of water vapor is lower than about 2 mols per mol of phenol the effect on ex tending catalyst life is decreased. On the other hand, when the ratio increased appreciably above 12:1 the partial pressure of the phenol decreases and this in turm reduces the space-time yield of methylated products.

The reaction pressure is not critical. It may be carried out at atmospheric pressure, and may also be carried out over a wide range of pressure varying from about 0.5 to 50 atmospheres.

Best catalytic activity and optimum selectivity is achieved by maintaining the gas space velocity at from about 360 to 18,000 hr". The preferred range from the viewpoint of economical operation is 900 to 12,000 hr". Generally the gas space velocity will be on the high side of the range at higher temperatures and will be decreases as the operating temperature decreases.

A number of other oxides and oxide mixtures have been tested for their catalytic activity and have not been found to have useful activity. Silica, for example, has virtually no activity. lron oxide mixed with phosphorous oxide, selenium oxide or tellurium oxide were also without practical value.

The following non-limiting examples are given by way of illustration only. In the examples the following definitions apply:

Yield based on the phenol in the feed (percent) the phenol in the feed (mol/hr.)

Yield based on the converted phenol (perm-tit) desired produgtlmol/lml X the phenol in feed (mol/hr.)

the unreaeted phenol (mol/hr.

Yield based on converted methanol (percent) desired product (mol/hr.) number of methyl ggu s in desired product Hm the phenol in feed (mol/hr.)

-1mreacted methanol (mol/hf.)

The pressure loss represented by AP is the differential pressure across the ends of the catalyst layers. It is measured with a manometer.

EXAMPLE 1 Preparation of Catalyst Twenty g. of ammonium metavanadate and 5 g. of oxalic acid are dissolved in 40 cc. of pure water and heated over a boiling water bath to dryness. The dried mass is then heated at 550C. for three hours in an air stream. The resultant material is ground to 16 32 mesh particles and used as the catalyst.

Reaction A mixture of methanol and phenol in the molar proportion 5 l and nitrogen gas are continuously supplied at a rate 7.9 cc/hr. and 17.7 cc/min. respectively through a preheater maintained at 220C. in which the feed is vaporized, to a pyrex glass reactor having a 1.8 cm internal diameter containing 1.2 cc. of the catalyst. The reactor is uniformly maintained at 350C. The reaction is carried out for 50 hours with the gas space velocity of the feed controlled at 9,000 hrs. The resultant product is gas-liquid separated by means of air-cooled traps and dry-ice traps (-78C.). Gas and liquid are individually analyzed with gas chromatography. According to the analysis, the conversion of phenol was 50.5percent and the yield of o-cresol and 2,6-xylenol were 62.1percent and 28.4percent respectively based on the phenol converted.

Similar results are obtained with o-cresol and with 2,3-xylenol.

EXAMPLES 2-6 Preparation of Catalyst 15.6 g. of vanadium trichloride are dissolved in a 100 cc. of pure water. The solution is then agitated, and 24 cc. of 14 percent aqueous ammonia is added dropwise until pH of the solution increases to 6.8. The precipitate formed is washed with water, filtered and then dried for 24 hours at 100C. The resultant mass is heated for three hours at 650C. and used as the catalyst.

Reactions Five runs are made as according to Example 1, using 1.2 cc. of thus prepared catalyst on the feed having molar ratio of methanol to phenol of 3 l, and 5 l and that of methanol to phenol to water of 3 l 3, 3 l 5 and 5 l 3, respectively. The results are shown in Table 1. In Table AP is the differential pressure across the catalyst layer. An increase of AP is to be avoided to ensure continued operation. It is observed that the water added effectively inhibited the catalyst particles from breaking into pieces.

EXAMPLES 7-8 Example 1 is repeated to methylate o-cresol with methanol except that the molar ratio of methanol to ocresol and methanol to o-cresol to water in each feed is 3 1 and 3 z 1 z 3, respectively. The results are shown in Table 2.

EXAMPLE 9 Preparation of Catalyst In 100 cc. of pure water, there are dissolved 2.9 g. of ammonium metavanadate, 2 g. of oxalic acid and 10.0 g. ferric nitrate represented by Fe(NO :9H O. The solution is added with stirring to 378 g. of ALUMINA- SOL (Trademark; manufactured by Nissan Kagaku Kogyo K.K.) containing 10 percent by weight of aluminum oxide, to which is then added dropwise 13 cc. of aqueous ammonia until the pH of the solution increases to 6.8. The precipitate which forms is washed with water, filtered, dried at l 10C. for 24 hours and heated at 450C. for three hours. The resultant particles are pulverized to the size of 16-32 mesh and used as the catalyst. The atomic ratio of iron to vanadium in the thus prepared catalyst is 2:1, the total amount of vanadium pentoxide and ferric oxide as carried on aluminum oxide being 10 percent by weight based on aluminum oxide.

Reaction Repetition of Example 1 using 5 cc. of the catalyst prepared as above gave 78.4 percent of converted phenol and the yields of o-cresol and 2,6-xylenol are 72.6 percent and 24.2 percent, respectively, based on the converted phenol. Similar results are obtained with pcresol and 3,4,5-trimethylphenol.

EXAMPLES 10-16 Preparation of Catalyst One hundred g. of ferric nitrate (Fe(NO .9H O) is dissolved in 200 cc. of pure water and 94 cc. of 14 percent aqueous ammonia added to the solution so that the pH of the solution increases to 6.8. The precipitate which forms is washed with water and filtered. Twentyfive g. of the precipitate is added to 50 cc. of an aqueous solution containing 7.2 g. of ammonium metavanadate and l g. of oxalic acid dissolved therein. The resultant solution is concentrated to dryness over a boiling water bath. The dried mass is sieved to give 16-32 mesh particles, which are then heated at 450C. for three hours while air is passed over them to give the catalyst. The atomic ratio of iron to vanadium of the catalyst is l 1. Other catalysts having various atomic ratios are prepared in the same manner.

Reaction Example 1 is repeated using seven different catalysts prepared in accordance with the example. The results are shown in Table 3.

Example 17-20 Preparation of Catalyst One hundred grams of ferric nitrate is dissolved in 200 cc. of pure water, and 94 cc. of 14 percent aqueous ammonia added dropwise to the resultant solution until the pH of the solution reaches 6.8. The precipitate which forms is washed with water and filtered. Twenty five g. of the thus obtained precipitate is added to 50 cc. of an aqueous solution of ammonium metavanadate. The resultant solution is concentrated to dryness over a hot water bath. The dried mass is sieved to 16-1- 6-32 mesh particles, which are heated at 650C. for three hours under passing air to give the catalyst. The atomic ratio of iron to vanadium in the catalyst is l 1. Other catalysts of various atomic ratios are prepared in the similar manner.

Reaction Six runs are made in accordance with Example 1 except that the compositions of feeds are varied. Example 17 is run on a mixture of methanol with phenol in the molar ratio of 5 1, while Examples 18-22, are run on a mixture of methanol, phenol and water in the molar ratio of 5 1 z 3, respectively. The results measured after passage of reaction hours are shown in Table EXAMPLE 23 Preparation of Catalyst In 100 cc. of pure water, there are dissolved 7.8 g. of vanadium trichloride and 10.0 g. of ferric nitrate. Then, 18 cc. of 14 percent aqueous ammonia are added dropwise to the resultant solution until the pH of the solution increases to 6.8. The precipitate formed is then washed with water, filtered and dried at l 10C. fo 24 hours. The dried material is heated at 650C. for three hours in the air stream to give ghe catalyst.

The atomic ratio of iron to vanadium of the catalyst is 0.5 1.

Reaction The reaction is carried out on a mixed feed of methanol, phenol and water in the molar proportion of 8 l 6, using 2 cc. of the catalyst. The mixture feed is supplied to the reactor at a rate of 7.9 cc./hr. The procedure is similar to Example 1, but the nitrogen carrier gas is omitted.

A comparative test is run by repeating the same procedure except that the water is replaced by nitrogen in the same mol fraction. The result obtained after the passage of 48 hours is shown in Table 5.

EXAMPLES 24-34 Preparation of Catalyst In 200 cc. of pure water are dissolved 21.4 g. of ammonium metavanadate and 34.4 g. of ferrous sulfate (FeSO .7H O). The resultant solution is added, all at one time, with stirring to 86 cc. of 14 percent aqueous ammonia with stirring to form a precipitate. The precipitate is washed with water. filtered, dried for 24 hours at l 10C. and further heated another three hours at 650C. in the air stream to give the catalyst. The atomic ratio of iron to vanadium of the catalyst is l 1.

Reaction Example 1 is repeated using 2 cc. of catalyst for each run on the feed of various compositions. The feed is supplied at a rate of 7.9 cc./hr. at a room temperature.

The results obtained after the passage of 100 hours are shown in Table 6.

EXAMPLE 35 Preparation of Catalyst An aqueous solution prepared by dissolving 69.1 g. of ferric nitrate in 150 cc. of pure water is added with stirring to an aqueous solution of 20.0 g. of ammonium metavanadate and 6 g. of oxalic acid dissolved in 150 cc. of pure water. To the resultant solution there is added dropwise 55 cc. of 14 percent aqueous ammonia until the pH of the solution increases to 6.8. The precipitate which forms is washed with water, filtered, dried for 24 hours at 1 C. and further heated for another three hours in an air stream, to give the catalyst. The atomic ratio of iron to vanadium of the catalyst is 1 1.

Reaction Example 1 is repeated for 600 hours on a feed mixture of methanol, phenol and water in the molar ratio of 8 l 6. The changes measured with the passage of reaction times are shown in Table 7.

EXAMPLE 36 Methylation of o-cresol with methanol is made in the presence of the catalyst as in Example 13 having an atomic ratio of iron to vanadium of 1:1. Example 1 is repeated on the feed of which molar ratio of phenol to o-cresol is 3 l, to give o-cresol conversion of 95.8 percent and a yield of 2,6-xylenol bases on converted ocresol of 97.5 percent. Similar results are obtained when the nitrogen is replaced with methane.

EXAMPLE 37 O-cresol is methylated with methanol, using the catalyst as prepared in Example 24. Example 1 is repeated on a feed containing methanol. o-cresol and water in the proportion of 3 l 3. After 100 hours, AP reaches 9.5 cm. H O, o-cresol conversion is 85.8% and the yield of 2,6-xylenol is 83.4 percent.

EXAMPLE 38 Methylation of phenol and o-cresol with methanol is made using the catalyst as prepared in Example 13. Example l is repeated except that the molar ratio of methanol to phenol is 4 1 and phenol to O-cresol is 2 1. An analysis of product liquid shows 12.4 percent of phenol, 24.1 percent of o-cresol and 61.4 percent of 2,6-xylenol.

EXAMPLE 39 EXAMPLES 40-47 Preparation of Catalyst In 130 cc. of water there are dissolved 25.0 g. of ferric nitrate (Fe(NO .9H O), 7.2 g. of ammonium metavanadate and 5 g. of oxalic acid. To the resultant solution there are added 20 cc. of an aqueous solution of 1.59 g. of magnesium nitrate (Mg(NO .6H O). The pH of the solution is increased to 6.8 by adding 32 cc. of 14 percent aqueous ammonia with stirring. The precipitate which forms is washed with water, filtered, dried at l 10C. for 24 hours and heated at 450C. for another three hours. The atomic ratio of iron to vanadium of the catalyst is 1, magnesium to iron is 0.1 1. Another catalyst containing titanium oxide is prepared by repeating the above operation with titanium tetrachloride substituted for magnesium nitrate. Anothe catalyst containing magnesium oxide and titanium oxide is prepared in a similar manner by adding magnesium nitrate and titanium tetrachloride.

Reaction Example 1 is repeated using catalysts as tabulated in Table 8.

EXAMPLE 48-54 Preparation of Catalyst In 150 cc. water there are dissolved 25.0 g. ferric nitrate, 7.2 g. of ammonium metavanadate, 5 g. oxalic acid and 4.67 g. manganese nitrate (Mn(NO .4H O). With stirring, 36 cc. of 14 percent aqueous ammonia is added dropwise until the pH of the solution increases to 6.8. The precipitate formed is washed with water, filtered, dried at 1 10C. for 24 hours, and heated at 450C. for another three hours, to give the catalyst. The atomic ratio of iron to vanadium of thus prepared catalyst is 1, and that of manganese to iron is 0.3 1.

In similar manner, a number of catalysts having different composition are prepared.

Reaction Seven runs are made in accordance with Example 1 using seven different catalysts and the results are tabulated in Table 9.

EXAMPLES 55-68 Preparation of Catalyst In cc. of water there are dissolved 25.0 g. ferric nitrate, 7.2 g. ammonium metavanadate and 5 g. oxalic acid. To the resultant solution is then added 30 cc. of an aqueous solution containing 1.59 g. magnesium nitrate, 1.17 g. titanium tetrachloride and 4.67 g. manganese nitrate. With agitation, 41 cc. of 14 percent aqueous ammonia are added dropwise to the resultant mixture solution until the pH reaches 6.8. The precipitate formed is washed with water, filtered, dried at l 10C. for 24 hours and heated at 450C. for three hours, to give the catalyst.

The various atomic ratios in the catalyst are as follows: Fe/V l, Mg/Fe 0.1, Ti/Fe 0.1 and Mn/Fe 0.1.

In a similar manner an additional 13 catalysts of different compositions are prepared.

Reaction In each run, Example 1 is repeated using the catalyst prepared as above. Results are shown in Table 10.

EXAMPLE 69 Methylation is carried out for 1800 hours in succession using the catalyst as prepared in Example 62. The composition of the catalyst is such that Fe/V l, Mg/Fe Ti/Fe 0.1, Mn/Fe 0.3. Example 1 is repeated using 5 cc. of the catalyst on the feed having a methanol, phenol, water ratio of 8 l 6. Results are shown in Table 11.

EXAMPLE 70 Preparation of Catalyst Reaction Repetition of Example 1 using thus prepared catalyst gives, after 100 hours, 79.8 percent phenol conversion and 40.0 percent yield of 2,6-xylenol based on phenol in the feed.

EXAMPLE 71 Preparation of Catalyst Twenty five g. of ferric nitrate, 47.2 g. of ammonium metavanadate, and 5 g. of oxalic acid are dissolved in 150 cc. of water. To the resultant solution is added dropwise with stirring, 24 cc. of 14 percent aqueous ammonia until the pH of the solution reaches 6.8. The precipitate formed is washed with water, filtered, a solid lump is obtained. The lump is suspended in 50 cc. of water, to which 1.15 g. boric acid is added and the whole dried over a boiling water bath, dried at l C. for 24 hours and heated at 450C. for three hours. The atomic ratio of iron to vanadium is l 1, that of boron to iron being 0.3 1.

Reaction Example 1 is repeated using the thus prepated catalyst, giving 81.2 percent phenol conversion. The yield of 2,6-xylenol based on phenol in the feed is 39.6 percent and the total yield of o-cresol plus 2,6-xylenol based on converted methanol is 49.6 percent.

EXAMPLE 72 Methylation of o-cresol with methanol is made in accordance with Example 1 using the same catalyst as prepared in Example 64 on a feed material containing methanol, o-cresol and water in a molar proportion of 3 l 3. One hundred and twenty hours of reaction gives 88.9 percent o-cresol conversion. The yield of 2,6-xylenol based on o-cresol in the feed material is 87.4 percent.

EXAMPLE 73 A mixture of phenol and o-cresol is methylated with methanol using 2 cc. of the same catalyst as prepared in Example 64, in accordance with Example I on a feed containing methanol, phenol, o-cresol and water in a molar proportion of 4 l 2 6. After 100 hours, AP reaches 3.6 cm H O. The composition of the liquid product as analyzed by a gas chromatography is 2.5 percent phenol, 13.9 percent o-cresol and 82.2 percent of 2,6-xylenol.

EXAMPLE 74 Preparation of Catalyst To 150 cc. of an aqueous solution of 10 percent oxalic acid is added 27 g. vanadium pentoxide, which is then dissolved by heating the mixture at C. The solution is concentrated to dryness over a boiling water bath and heated at 500C. for three hours under passing air, giving vanadium oxide which is used as the catalyst. Repetition of the experiment of Example I using this catalyst gives, after 48 hours of reaction, 45.8 percent phenol conversion. The yields of o-cresol and 2,6- xylenol based on converted phenol are 63.3 percent and 27.9 percent respectively. Similar results are obtained with 2-xylylphenol and 2-tolyl-4-phenylphenol.

EXAMPLE 75 Preparation of Catalyst To 150 cc. of a 10 percent oxalic acid aqueous solution is added 18 g. of vanadium pentoxide and 15.8 g. of ferric nitrate, which are then heated for dissolving. The resultant solution is concentrated to dryness over a boiling water bath. The dried material is heated at 500C. for three hours under passing air to give vanadium oxide catalyst. The atomic ratio of iron to vanadium of the catalyst is l 1.

Reaction:

Example 1 is repeated using the thus prepared catalyst to give, after 50 hours, 65.4 percent phenol conversion. The yields of o-cresol based on converted phenol and that of 2,6-xylenol based on converted phenol are 66.8 percent and 30.2 percent, respectively.

Table 1 Reaction Yield Based on Example Feed Com%1 ition gmole) Time AP Phenol Phenol in Feed No. me ano e ano water (hr.) (cm H O) Conversion oreso y eno 2 3 l I00 10.25 27.l 21.3 4.1 3 3 I 3 97 20.1 28.3 20.7 5.3 4 3 l 5 102 7.2 34.9 23.8 8.4 5 5 l 101 84.6 45.7 29.0 l3.l 6 5 l 3 I00 I33 48.2 27.9 l5.6

Table 2 Example Feed Compgsition imolg) Reaction AP o-Cresol Yield of 2.6-Xylene Based No. me and o-creso water Time (hr.) (cmH O) Conversion on o-Cresol in Feed 7 3 l 100 99.2 55.2 5L3 8 3 l 3 mo 12.0 58.6 53.3

Table 3 Yield Based on Phenol in Yield of o-Cresol and 2,6-Xylenol Atomic ratio Feed LZz) Example of Catalyst Phenol Based on Based on No. V/Fe Conversion o-Cresol 2,6-Xy1enol Converted Phenol Converted Methanol 1/9 48.8 27.5 14.5 86.2 28.8 11 1/4 71.8 38.7 31.4 97.7 34.8 12 1/2 89.4 52.6 34.8 98.9 35.4 13 III 91.5 47.2 39.7 97.4 41.6 14 2/1 73.9 38.9 32.4 98.2 38.4 15 4/1 70.4 37.1 32.0 98.1 40.3 16 9/1 64.2 35.8 20.2 93.4 29.2 Comparative Test Fe 9.2 7.0 0.7 83.4 13.4

Table 4 Yield Based on Phenol Total Yield of o-Cresol Example Atomic ratio of AP Phenol in Feed 1%) and 2,6-Xylenol Based No Catalyst (V/Fe) Water (cm Hp) Conversion o-Cresol 2.6-Xylenol on Converted Phenol 17 Ill 72.8 89.9 47.5 40.8 98.2 18 1/9 Added 4.3 67.3 37.3 21.9 88.1 19 1/2 do 6.0 90.2 51.7 37.1 98.6 20 1]! do 6.4 93.8 45.4 46.5 98.0 21 2/1 do 7.8 77.4 38.8 37.2 98.2 22 9/1 do 16.7 71.8 39.6 27.0 92.7

Table 5 Yield Based on Phenol Example Feed Commgition Molar Ratio) AP Phenol m Feed No. et ano eno ater ltrogen (cm H O) Conversion oreso yeno 23 8 l 6 4.1 99.0 8.8 85.9 Com arative est 8 l 6 53.6 88.2 23.4 64.0

Table 6 Example Feed Commsition lMolar Ratio) P Phenol Yield Based on Phenol in F No. e ano eno ater (cm H O) Conversion reso y eno Table 7 Example Reaction P Phenol Yield Based on Phenol in Feed 5%) No. Time (hr.) (cm H O) Conversion reso y eno Table 8 Composition Yield Based on Phenol Total Yield of o-Cresol and 2 6X lenol Example of Ca tal st Reaction Phenol in Feed on use on No. in Atomic tio Time (hr.) Conversion oreso y eno Converted Phenol Converted Methanol r 97.4 23.0 72.1 97.7 40.1 40 v Fe Mg 5 90.2 25.8 62.8 98.2 38.8 50 89.8 28.1 60.3 98.5 37.9

5 86.1 26.2 58.5 98.3 36.2 41 V Fe Mg 48 85.3 32.1 52.2 98.8 34.6

5 88.5 29.2 57.9 98.4 38.4 42 V Fe Mg 46 86.9 29.9 55.7 98.5 37.9

5 95.8 13.9 76.7 94.6 31.0 43 V FeMg 50 81.1 41.7 38.4 98.7 29.8

1 96.9 33.9 60.9 97.9 38.4 44 V,Fe,Ti 5 90.6 35.6 53.7 98.6 37.2 50 88.8 36.4 51.1 98.6 36.9

5 85.4 33.7 50.3 98.4 36.1 45 V Fe TiM 81.6 37.5 43.0 98.7 33.3

1 96.8 25.8 69.0 97.9 40.7 46 V F6 Mgo o.n5 5 87.2 27.1 58.6 98.3 40.0 50 86.5 27.8 57.4 98.5 38.7

1 96.4 32.5 62.0 98.0 39.4 47 v.r=e,M .,.,Ti., 5 89.5 33.2 54.7 98.2 38.2 50 87.8 34.1 52.3 98.5 37.6

Table 9 Yield Based on Phenol Example Composition of Phenol in Feed a! on use on No. Catalyst (Atomic Ratio) Conversion oreso ,6-Xylenol Converted Phenol Converted Methanol 48 v Fe Mn 94.0 25.4 66.1 97.3 49.8 49 V,Fe Mn 93.8 25.8 65.5 97.3 50.6 50 V,Fe,Mn 89.7 27.2 60.3 97.5 51.1 51 V,Fe Mn 84.1 30.1 52.4 98.1 49.7 52 V Fe,Mn, 80.9 36.4 44.0 98.4 48.3 53 v Fe Mn 90.6 30.8 57.4 97.4 48.9 54 V Fe,Mn 96.2 16.9 73.8 94.4 42.2

Table 10 Composition of Yield Based on Phenol in Total Yield of o-Cresol and 2.6-Xv1erol(%) Example Catalyst (Atomic Ratio) Phenol Feed Based on Based on No. V Fe: Mg Ti Mn Conversion reso y eno Converted Phenol Converted Methanol 55 l 1 :0.1 :0 0.3 86.6 39.0 45.8 97.9 50.9 56 1 1 0.1 0 0.5 81.4 37.5 42.5 98.2 48.2 57 1 1 :0.3 :0 0.3 82.6 36.8 43.6 97.3 44.5 58 1 1 :0.3 :0 0.5 78.3 36.0 40.8 98.1 47.1 59 1 1 :0 z 0.1 :0.3 86.0 35.8 49.2 98.8 50.7 60 1 1 :0 0.1 :0.5 84.3 37.7 45.6 98.8 48.2 61 l 1 :0.1 10.1 :0 87.9 35.4 50.4 97.6 36.4 62 l 1 :0 0.3 0.5 76.5 37.5 38.1 98.9 46.3 63 l l :0.1 :0.1 10.1 87.3 25.8 60.2 98.5 49.0 64 1 1 :0.1 :0.1 10.3 89.9 26.1 62.4 98.4 51.2 65 1 l :0.1 :0.1 10.5 88.3 28.5 58.1 98.1 50.6 66 1 l :0.1 10.1 :0.7 80.8 29.5 50.2 98.6 50.8 67 l 2 0.1 0.1 20.3 86.5 28.0 56.5 97.7 47.7 68 2: 1 20.1 :0.1 10.3 93.2 19.7 70.1 96.3 41.3

Table 11 Example Reaction AP Phenol Yield Based on Phenol in Feed No. Time (hr.) (cm H O) Conversion reso y eno What is claimed is:

l. A process of methylating a phenol in the ortho position which comprises reacting methanol with a phenol having the formula 3. A process as in claim 2 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about l/9-9: l l 0.01.

4. A process as in claim 1 wherein the reaction mixture contains from about 2 to 12 mols of water vapor per mol of phenol reactant.

5. A process as in claim 1 wherein the molar ratio of methanol to phenol reactant is from about 1 l to 10 l.

6. A process as in claim 1 wherein the temperature is from 300C. to 400C.

7. A process of methylating phenol in the ortho position which comprises reacting methanol with phenyl in the vapor phase in the presence of a vanadium oxide catalyst at a temperature of from about 250C. to 450C.

8. A process as in claim 7 wherein the catalyst is a metallic oxide containing iron and vanadium in the atomic ratio of from about 9 to H9.

9. A process as in claim 8 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about l/9-9: l l 0.01.

10. A process as in claim 7 wherein the reaction mixture contains from about 2 to l2 mols of water vapor per mol of phenol.

11. A process as in claim 7 wherein the molar ratio of methanol to phenol is from about 1 l to 10 l.

12. A process as in claim 7 wherein the temperature is from 300C. to 400C.

13. A process of methylating o-cresol in the ortho position which comprises reacting methanol with o-eresol in the vapor phase in the presence of a vanadium oxide catalyst at a temperature of from about 250C. to 450C 14. A process as in claim 13 wherein the catalyst is a metallic oxide containing iron and vanadium in the atomic ratio of from about 9 to l/9.

15. A process as in claim 14 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about l/9-9: l l 0.0].

16. A process as in claim 13 wherein the reaction mixture contains from about 2 to l2 c8 mols of water vapor per mol of o-cresol.

17. A process as in claim 13 wherein the molar ratio of methanol to o-cresol is from about I l to 10 1 l.

18. A process as in claim 13 wherein the temperature is from 300C. to 400c. 

1. A PROCESS OF METHYLATING A PHENOL IN THE ORTHO POSITION WHICH COMPRISES REACTING METHANOL WITH A PHENOL HAVING THE FORMULA
 2. A process as in claim 1 wherein the catalyst is a metallic oxide containing iron and vanadium in the atomic ratio of from about 9 to 1/9.
 3. A process as in claim 2 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about 1/9-9: 1 : 1 - 0.01.
 4. A process as in claim 1 wherein the reaction mixture contains from about 2 to 12 mols of water vapor per mol of phenol reactant.
 5. A process as in claim 1 wherein the molar ratio of methanol to phenol reactant is from about 1 : 1 to 10 :
 1. 6. A process as in claim 1 wherein the temperature is from 300*C. to 400*C.
 7. A process of methylating phenol in the ortho position which comprises reacting methanol with phenyl in the vapor phase in the presence of a vanadium oxide catalyst at a temperature of from about 250*C. to 450*C.
 8. A process as in claim 7 wherein the catalyst is a metallic oxide containing iron and vanadium in the atomic ratio of from about 9 to 1/9.
 9. A process as in claim 8 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about 1/9-9: 1 : 1 - 0.01.
 10. A process as in claim 7 wherein the reaction mixture contains from about 2 to 12 mols of water vapor per mol of phenol.
 11. A process as in claim 7 wherein the molar ratio of methanol to phenol is from about 1 : 1 to 10 :
 1. 12. A process as in claim 7 wherein the temperature is from 300*C. to 400*C.
 13. A process of methylating o-cresol in the ortho position which comprises reacting methanol with o-cresol in the vapor phase in the presence of a vanadium oxide catalyst at a temperature of from about 250*C. to 450*C
 14. A process as in claim 13 wherein the catalyst is a metallic oxide containing iron and vanadium in the atomic ratio of from about 9 to 1/9.
 15. A process as in claim 14 wherein the catalyst contains iron, vanadium, and at least one other metal selected from the group consisting of manganese, magnesium, titanium, beryllium and boron wherein the atomic ratio of vanadium to iron to other metal or mixture thereof is from about 1/9-9: 1 : 1 - 0.01.
 16. A process as in claim 13 wherein the reaction mixture contains from about 2 to 12 c8 mols of water vapor per mol of o-cresol.
 17. A process as in claim 13 wherein the molar ratio of methanol to o-cresol is from about 1 : 1 to 10 :
 1. 18. A process as in claim 13 wherein the temperature is from 300*C. to 400*c. 